Process for preparing a catalyst component for polymerization of olefins

ABSTRACT

The present invention relates to a process for preparing a catalyst component for polymerization of an olefin comprising the steps of: i) contacting a compound R 9   z MgXz 2-z  wherein R 9  is aromatic, aliphatic or cyclo-aliphatic group containing up to 20 carbon atoms, X is a halide, and z is in a range of larger than 0 and smaller than 2, with an alkoxy- or aryloky-containing silane compound pound to given first intermediate reaction product; ii) contacting the first intermediate reaction product with at least one activating compound selected from the group formed by electron donors and compounds of formula M(OR 10 ) v-w (OR 11 ) w , wherein M can be Ti, Zr, HI, Al or Si, and M(OR 10 ) v-w (R 11 ) w , wherein M is Si, each R 10  and R 11 , independently, represent an alkyl, alkenyl or aryl group, v is the valency of M, v being either 3 or 4, and w is smaller than v, to give a second intermediate reaction product; and iii) contacting the second intermediate reaction product with a halogen-containing Ti-compound, a monoester as activating agent, a 1,3-diether as an internal electron donor, and optionally a diester as an additional internal electron donor.

The invention relates to a process for preparing a catalyst componentfor polymerization of an olefin. Furthermore, the invention relates tocatalyst component obtainable by said process. The invention alsorelates to a process for making a polyolefin by contacting an olefinwith a catalyst system containing said catalyst component and to apolyolefin. The invention also directs to use of said catalyst componentfor polymerization of an olefin.

Document EP2027164B1 discloses a process for preparing a polymerizationcatalyst component comprising the steps of i) contacting a compound R⁴_(z)MgX_(2-z) wherein R⁴ is an organic group, X is a c, and z is largerthan 0 and smaller than 2, with an alkoxy- or aryloxy-containing silanecompound to give a solid magnesium-containing compound of formulaMg(OR¹)_(x)Cl_(2-x) wherein x is larger than 0 and smaller than 2, andeach R¹, independently, represents an alkyl group; ii) contacting thesolid Mg(OR¹)_(x)Cl_(2-x) with at least one activating compound selectedfrom the group formed by electron donors and compounds of formulaM(OR²)_(v-w)(R³)_(w), wherein M can be Ti, Zr, Hf, Al or Si, each R² andR³, independently, represent an alkyl, alkenyl or aryl group, v is thevalency of M and w is smaller than v, in the presence of an inertdispersant to give an intermediate reaction product, and iii) contactingthe intermediate reaction product with a halogen-containing Ti-compoundand an internal electron donor. The polypropylene obtained by using thecatalysts prepared by the process disclosed in EP2027164B1 show limitedhydrogen sensitivity.

The ‘Ziegler-Natta catalyst’ term is well-known in the art and typicallyrefers to catalyst systems comprising a transition metal containingsolid catalyst component (also generally referred to in the prior art asprocatalyst or catalyst precursor); an organo-metal component asco-catalyst and, optionally, one or more electron donor components (e.g.external donors). The transition metal containing solid catalystcomponent comprises a transition metal halide, i.e, titanium, chromium,vanadium halide supported on a metal or metalloid compound, such asmagnesium chloride or silica. An overview of different catalyst types isfor example given by T. Pullukat and R. Hoff in Catal. Rev.—Sci. Eng.41, vol. 3 and 4, 389-438, 1999.

Other processes to prepare Ziegler-Natta catalyst components suitablefor polymerization of olefins are also disclosed in the art. DocumentWO96/32426A discloses a 3-step process for producing a catalyst for thepolymerization of an olefin, wherein in the first two steps a compoundMg(OAlk)_(x)Cl_(y) of certain morphology is prepared, and subsequentlythis solid Mg-compound is contacted with titanium tetrachloride, and anelectron-donating compound. EP398698A1 also discloses a process forpolymerization of an olefin in the presence of a solid catalystcomponent, which is obtained by first reacting Mg(OR¹)_(n)(OR²)_(2-n),Ti(OR³)₄, Ti(OAlk)₄ and SI(OR⁴)₄ in solution to form an intermediateproduct, which is further contacted with TiX_(m)(OR⁶)_(4-m) and anelectron donating compound EP1838741B1 discloses a process for producinga catalyst for the polymerization of an olefin, wherein a compound withformula Mg(OAlk)_(x)Cl_(y), wherein x is larger than 0 and smaller than2, y equals 2-x and each Alk, independently, represents an alkyl group,is contacted with a titanium tetraalkoxide and/or an alcohol in thepresence of an inert dispersant to give an intermediate reaction productand wherein the intermediate reaction product is contacted with titaniumtetrachloride in the presence of an internal donor. DocumentWO02/100904A1 discloses solid catalyst components comprising Ti, Mg,halogen and an internal electron compound selected from 1,3-diethers.However, the polyolefins obtained by using the catalysts prepared byapplying the processes disclosed in these documents show limitedhydrogen sensitivity. US6395670B1 discloses catalyst components for thepolymerization of olefins having Mg, Ti, halogen and at least twointernal electron donor compounds selected from esters containing atleast two ether groups and esters of mono or polycarboxylic acids.

There is however an on-going trend in industry towards polymericmaterials having high melt flow rates (MFR) which maintain a highstereospecificity. Higher MFR means better processability of the polymermaterial, i.e. due to good flowability. High MFR of polymers can beobtained by using peroxides during polymer granulating (palletizing).But this leads to narrower MWD of the polymer obtained. Therefore higherMFR values at polymerization are desired. Hydrogen can also be added topolymerization reactors to control MFR values. However, the use of highhydrogen concentration for high MFR is not desirable due totechnological problems at polymer, e.g. polypropylene production incommercial reactors. Therefore catalysts with higher hydrogensensitivity (hydrogen response) providing high MFR at the same hydrogenconcentration are important.

Thus, faster throughput of the process for producing end applicationarticles from the polymer, and therefore cost savings, can be achieved.In addition, the xylene solubles, which consist primarily of amorphous(atactic) polymer and oligomers typically increase with increasing MFR,which is not desirable for many applications, for instance in theautomotive field and packaging area for food and medicals. Polymers withhigh stereospecifity are polymers having high isotacticity and thus lowamount of atactic polymer fraction. It is already known that thepresence of a high atactic fraction in the polymer can deteriorate theproperties of the final product, such as decreasing the strength of thematerials and also migrating to the material surface causing forinstance blooming. Therefore, polymers with high MFR and still highisotacticity, i.e. low atactic polymer content are becoming increasinglyimportant.

It is thus an object of the invention to provide a catalyst forpolymerization of an olefin, which allows obtaining polyolefins,especially polypropylene having high melt flow rate and highisotacticity.

This object is achieved with a process for preparing a catalystcomponent for polymerization of an olefin comprising the steps of:

i) contacting a compound R⁹ _(z)MgX_(2-z) wherein R⁹ is aromatic,aliphatic or cyclo-aliphatic group containing up to 20 carbon atoms, Xis a halide, and z is in a range of larger than 0 and smaller than 2,with an alkoxy- or aryloxy-containing silane compound to give a firstintermediate reaction product;

ii) contacting the first intermediate reaction product with at least oneactivating compound selected from the group formed by electron donorsand compounds of formula M(OR¹⁰)_(v-w)(OR¹¹)_(w), wherein M can be Ti,Zr, Hf, Al or Si, and M(OR¹⁰ )_(v-w)(R¹¹)_(w), wherein M is Si, each R¹⁰and R¹¹, independently, represent an alkyl, alkenyl or aryl group, v isthe valency of M, v being either 3 or 4, and w is smaller than v, togive a second intermediate reaction product; and iii) contacting thesecond intermediate reaction product with a halogen-containingTi-compound, a monoester, a 1,3-diether as an internal electron donor,and optionally, a diester as an additional internal electron donor.

In an embodiment, this object is achieved with a process for preparing acatalyst component for polymerization of an olefin comprising the stepsof:

i) contacting a compound R⁹ _(z)MgX_(2-z) wherein R⁹ is aromatic,aliphatic or cyclo-aliphatic group containing up to 20 carbon atoms, Xis a halide, and z is in a range of larger than 0 and smaller than 2,with an alkoxy- or aryloxy-containing silane compound to give a firstintermediate reaction product;

ii) contacting the first intermediate reaction product with at least oneactivating compound selected from the group formed by compounds offormula M(OR¹⁰)_(v-w)(R¹¹)_(w), wherein M is Si, each R¹⁰ and R¹¹,independently, represent an alkyl, alkenyl or aryl group, v is thevalency of M, v being either 3 or 4, and w is smaller than v, to give asecond intermediate reaction product; and

iii) contacting the second intermediate reaction product with ahalogen-containing Ti-compound, a monoester, a 1,3-diether as aninternal electron donor, and optionally, a diester as an additionalinternal electron donor.

It has been surprisingly found that the process according to the presentinvention allows preparation of polyolefins, particularly ofpolypropylenes (PP) having high MFR, for instance higher than 13, 15,20, 30 or 40 dg/min or even higher than 50 dg/min, and highisotacticity, for instance having an amount of atactic polymer of lowerthan 3, 2, 1 or 0.6 wt % or even lower than 0.5 wt %.

The key to the present invention is the combination of the use of amonoester—as activator—and a 1,3-diether—as internal donor—during thepreparation of a catalyst component. This inventive combination ofactivator and internal donor leads to a higher yield and a higher meltflow rate, while the molecular weight distribution remains the same oreven improves.

A further advantage of the process according to present invention isthat low amount of wax is formed, i.e. low molecular weight polymersduring the polymerization reaction, which results in reduced or no“stickiness” on the inside walls of the polymerization reactor andinside the reactor. In addition, the catalyst obtained by the processaccording to the invention has high hydrogen sensitivity. Furthermore,the polyolefins obtained by applying the catalyst obtained by theprocess according to the present invention have good yield.

SUMMARY OF THE PRESENT INVENTION

In a first aspect, the present invention relates to a process forpreparing a catalyst component for polymerization of an olefincomprising the steps of:

-   -   contacting a compound R⁹ _(z)MgX_(2-z) wherein R⁹ is aromatic,        aliphatic or cyclo-aliphatic group containing up to 20 carbon        atoms, X is a halide, and z is in a range of larger than 0 and        smaller than 2, with an alkoxy- or aryloxy-containing silane        compound to give a first intermediate reaction product;    -   contacting the first intermediate reaction product with at least        one activating compound selected from the group formed by        electron donors and compounds of formula)        M(OR¹⁰)_(v-w)(OR¹¹)_(w), wherein M can be Ti, Zr, Hf, Al or Si,        and)M(OR¹⁰)_(v-w)(R¹¹)_(w), wherein M is Si, each R¹⁰ and R¹¹,        independently, represent an alkyl, alkenyl or aryl group, v is        the valency of M, v being either 3 or 4, and w is smaller than        v; preferably the at least one activation compound is selected        from the group formed by compounds of formula        M(OR¹⁰)_(v-w)(R¹¹)_(w), wherein M is Si, to give a second        intermediate reaction product; and    -   contacting the second intermediate reaction product with a        halogen-containing Ti-compound, a monoester as activating agent,        a 1,3-diether as an internal electron donor, and optionally a        diester as an additional internal electron donor.

In an embodiment, the 1,3-diether is selected from the group consistingof 1,3-diethers with fluorenyl ligand without or with substituentshaving C1 to C10 carbon atoms.

In an embodiment, the 1,3-diether is 9,9-bis-methoxymethyl-fluorene.

In another embodiment, the molar ratio between the 1,3-diether of stepiii) and Mg is from 0.03 to 0.3.

In another embodiment, the monoester is an ester of an aliphaticmonocarboxylic acid with C1-C10 carbon atoms.

In another embodiment, the molar ratio between the monoester in stepiii) and Mg is from 0.05 to 0.5.

In another embodiment, the molar ratio between the monoester in stepiii) and Mg is from 0.15 to 0.25.

In another embodiment, the diester is a C1-10 aliphatic substitutedphthalate.

In another embodiment, the diester is dibutyl phthalate.

In another embodiment, the molar ratio between the diester of step iii)and Mg is from 0.03 to 0.15.

In another embodiment, the second intermediate reaction product iscontacted with a halogen-containing Ti-compound and then a monoester isadded, then a 1,3-diether as an internal electron donor, and thenoptionally a diester as an additional internal electron donor is added.

In another aspect, the present invention relates to a catalyst componentobtainable by the process according to the present invention comprisingTi, Mg, a halogen, a monoester, a 1,3-diether as an internal electrondonor and optionally a diester as an additional internal electron donor,preferably said monoester is present in an amount of less than 4.0 wt.%, more preferably in an amount of at most 3.5 wt. %.

In another aspect, the present invention relates to a catalyst systemfor polymerization of olefins comprising the catalyst componentaccording to the present invention, a co-catalyst and optionally anexternal electron donor.

In an embodiment, no external donor is present.

In another aspect, the present invention relates to a process for makinga polyolefin by contacting an olefin with the catalyst system comprisinga catalyst component prepared by the process for preparing a catalystcomponent according to the present invention.

In an embodiment, the olefin is propylene.

In another aspect, the present invention relates to the use of acatalyst component prepared by the process for preparing a catalystcomponent according to the present invention for polymerization of anolefin.

In another aspect, the present invention relates to a polyolefinobtained or obtainable by the process for making a polyolefin accordingto the present invention.

In an embodiment, said polyolefin is a polypropylene.

In an embodiment, said polyolefin is a homopolymer of propylene.

DETAILED DESCRIPTION OF THE PRESENT INVENTION

The present invention will be described in more detail below.

The process according to the present invention comprises several steps,which are discussed below.

Step i)

In step i) a first intermediate reaction product, i.e. a solidmagnesium-containing support is prepared by contacting a compound or amixture of compounds of formula R⁹ _(z)MgX_(2-z) wherein R° is aromatic,aliphatic or cyclo-aliphatic group containing up to 20 carbon atom, X isa halide, and z is larger than 0 and smaller than 2, with an alkoxy- oraryloxy-containing silane compound, as for example described in WO96132427 A1 and WO01/23441 A1. In the compound R⁹ _(z)MgX_(2-z), alsoreferred to as Grignard compound, X is preferably chlorine or bromine,more preferably chlorine. Preferably, R⁹ _(z)MgX_(2-z) isbutylmagnesiumchloride or phenylmagnesiumchloride.

Preferably, R⁹ is aromatic or aliphatic group containing 1 to 20 carbonatoms, preferably 1 to 10 carbon atoms; or cyclo-aliphatic groupcontaining 3 to 20 carbon atoms, preferably 3 to 10 carbon atoms. R⁹ ismore preferably an alkyl, aryl, aralkyl, alkoxide, phenoxide, etc., ormixtures thereof. Most preferably, R⁹ is methyl, ethyl, n-propyl,i-propyl, n-butyl, i-butyl, t-butyl, hexyl, cyclohexyl, octyl, phenyl,tolyl, xylyl, mesityl or benzyl. In a preferred embodiment of theinvention, R⁹ represents an aromatic group, for instance a phenyl group.The Grignard compound of formula R⁹ _(z)MgX_(2-z), wherein z is largerthan 0 and smaller than 2, is preferably characterized by z being fromabout 0.5 to 1.5.

The alkoxy- or aryloxy-containing silane used in step i) is typically acompound or a mixture of compounds with the general formula Si(OR¹³)_(4-n)R¹⁴ _(n), wherein n can range from 0 up to 3, preferably nis from 0 up to and including 1, and wherein each R¹³ and R¹⁴ groups,independently, represent an alkyl, alkenyl or aryl group, optionallycontaining one or more hetero atoms for instance O, N, S or P, with, forinstance, 1-20 C-atoms. Examples of suitable silane-compounds includetetramethoxysilane, tetraethoxysiiane, methyltrimethoxysilane,methyltributoxysilane, phenyltriethoxysllano. Preferably,tetraethoxysilane is used as silane-compound in preparing the solidMg-containing compound in the process according to the invention.Preferably, in step i) the silane-compound and the Grignard compound areintroduced simultaneously to a mixing device to result in particles ofadvantageous morphology, especially of the larger particles, asdescribed in WO 01/23441 A1. Here, ‘morphology’ does not only refer tothe shape of the particles of the solid Mg-compound and the catalystmade therefrom, but also to the particle size distribution (alsocharacterized as span), its fines content, powder flowability, and thebulk density of the catalyst particles. Moreover, it is well known thata polyolefin powder produced in polymerization process using a catalystsystem based on such catalyst component has a similar morphology as thecatalyst component (the so-called “replica effect”; see for instance S.van der Ven, Polypropylene and other Polyolefins, Elsevier 1990, p.8-10). Accordingly, almost round polymer particles are obtained with alengthidiameter ratio (I/D) smaller than 2 and with good powderflowability. Introduced simultaneously means that the introduction ofthe Grignard compound and the silane-compound is done in such way thatthe molar ratio Mg/Si does not substantially vary during theintroduction of these compounds to the mixing device, as described in WO01/23441 A1. The silane-compound and Grignard compound can becontinuously or batch-wise introduced to the mixing device. Preferably,the both compounds are introduced continuously to a mixing device.

It is explicitly noted that it is possible that the Grignard compound instep i) may alternatively have a different structure, for example, maybe complex. Such complexes are already known to the skilled person inthe art; a particular example of such complexes is Phenyl₄Mg₃Cl₂.

The mixing device can have various forms; it can be a mixing device inwhich the silane-compound is premixed with the Grignard compound, themixing device can also be a stirred reactor, in which the reactionbetween the compounds takes place. Preferably, the compounds arepremixed before the mixture is introduced to the reactor for step i). Inthis way, a catalyst component is formed with a morphology that leads topolymer particles with the best morphology (high bulk density, narrowparticle size distribution, (virtually) no fines, excellentflowability). The Si/Mg molar ratio during step i) may vary within widelimits for instance from 0.2 to 20. Preferably, the Si/Mg molar ratio isfrom 0.4 to 1.0.

The period of premixing in above indicated reaction step may varybetween wide limits, for instance 0.1 to 300 seconds. Preferablypremixing is performed during 1 to 50 seconds.

The temperature during the premixing step is not specifically critical,and may for instance range between 0 and 80° C.; preferably thetemperature is between 10° C. and 50° C. The reaction between saidcompounds may, for instance, take place at a temperature between −20° C.and 100° C.; preferably at a temperature of from 0° C. to 80 C.

The first intermediate reaction product obtained from the reactionbetween the silane compound and the Grignard compound is usuallypurified by rinsing with an inert solvent, for instance a hydrocarbonsolvent with for example 1-20 C-atoms, like pentane, iso-pentane, hexaneor heptane. The solid product can be stored and further used as asuspension in said inert solvent. Alternatively, the product may bedried, preferably partly dried, and preferably under mild conditions;e.g. at ambient temperature and pressure.

The first intermediate reaction product obtained by this step i) maycomprise a compound of the formula Mg(OR¹³)_(x)X_(2-x), wherein thegroup R¹³ is an alkyl containing 1-12 carbon atoms or an aryl groupcontaining 3-12 carbon atoms, although the present invention is notlimited thereby. X is a halide, and x is larger than 0 and smaller than2, preferably between 0.5 and 1.5. Preferably, X is chlorine or bromineand more preferably, X is chlorine,

Preferably, the R¹³ group contains 1-8 carbon atoms. More preferably, atleast one of the Fe³ groups represents an ethyl group. In a preferredembodiment, each R¹³ group represents an ethyl group.

R⁹ _(z)MgX_(2-z) used in step i) may be prepared by contacting metallicmagnesium with an organic halide R⁹X, as described in WO 96/32427 A1 andWO01/23441 A1. All forms of metallic magnesium may be used, butpreferably use is made of finely divided metallic magnesium, for examplemagnesium powder. To obtain a fast reaction it is preferable to heat themagnesium under nitrogen prior to use. R⁹ and X have the same meaning asdescribed above. Combinations of two or more organic halides R⁹X canalso be used.

The magnesium and the organic halide R⁹X can be reacted with each otherwithout the use of a separate dispersant; the organic halide R⁹X is thenused in excess. The organic halide R⁹X and the magnesium can also bebrought into contact with one another and an inert dispersant. Examplesof these dispersants are: aliphatic, alicyclic or aromatic dispersantscontaining from 4 up to 20 carbon atoms.

In this step of preparing R⁹ _(z)MgX_(2-z), also an ether can be addedto the reaction mixture. Examples of suitable ethers are: diethyl ether,diisopropyl ether, dibutyl ether, diisobutyl ether, diisoamyl ether,diallyl ether, tetrahydrofuran and anisole. Dibutyl ether and/ordiisoamyl ether are preferably used. Preferably, an excess ofchlorobenzene is used as the organic halide R⁹X. Thus, the chlorobenzeneserves as dispersant as well as organic halide R⁹X.

The organic halide/ether ratio acts upon the activity of the catalystcomponent. The chlorobenzene/dibutyl ether volume ratio may for examplevary between 75:25 and 35:65, preferably between 70:30 and 50:50.

Small amounts of iodine and/or alkyl halides can be added to cause thereaction between the metallic magnesium and the organic halide R⁹X toproceed at a higher rate. Examples of alkyl halides are butyl chloride,butyl bromide and 1,2-dibrornoethane. When the organic halide R₉X is analkyl halide, iodine and 1,2-dibromoethane are preferably used.

The reaction temperature for preparing R⁹ _(z)MgX_(2-z) normally isbetween 20 and 150° C.; the reaction time is normally between 0.5 and 20hours. After the reaction for preparing R⁹ _(z)MgX_(2-z), is completed,the dissolved reaction product may be separated from the solid residualproducts.

Step ii)

The first intermediate reaction product is contacted in step ii) with atleast one activating compound selected from the group formed by electrondonors and compounds of formula M(OR¹⁰)_(v-w)(OR¹¹)_(w), wherein M canbe Ti, Zr, Hf, Al or Si, and M(OR¹⁰)_(v-w)(R¹¹), wherein M is Si, eachR¹⁰ and R¹¹, independently, represent an alkyl, alkenyl or aryl group, vis the valency of M, being either 3 or 4, and w is smaller than v.

In an embodiment, the first intermediate reaction product is contactedin step ii) with at least one activating compound selected from thegroup formed by compounds of formula M(OR¹⁰)_(v-w)(R¹¹)_(w), wherein Mis Si, each R¹⁰ and R¹¹, independently, represent an alkyl, alkenyl oraryl group, v is the valency of M, being either 3 or 4, and w is smallerthan v.

The electron donor and the compound of formula M(OR¹⁰)_(v-w)(OR¹¹)_(w)and M(OR¹⁰)_(v-w)(R¹¹)_(w) may be also referred herewith as activatingcompounds.

Examples of suitable electron donors that can be used in step ii) areknown to the skilled person in the art and include alcohols, carboxylicacids and carboxylic acid derivatives. Preferably, an alcohol is used asthe electron donor in step ii). More preferably, the alcohol is a linearor branched aliphatic or aromatic having 1-12 carbon atoms. Even morepreferably, the alcohol is selected from methanol, ethanol, butanol,isobutanol, hexanol , xylenol and benzyl alcohol. Most preferably, thealcohol is ethanol or methanol.

Examples of suitable carboxylic acids include formic acid, acetic acid,propionic acid, butyric acid, isobutanoic acid, acrylic acid,methacrylic acid, maleic acid, fumaric acid, tartaric acid,cyclohexanoic monocarboxylic acid, cis-1,2-cyclohexanoic dicarboxylicacid, phenylcarboxylic acid, toluenecarboxylic acid, naphthalenecarboxylic acid, phthallc acid, isophthallc acid, terephthalic acidand/or trimellitic acid.

R¹⁰ and R¹¹ groups can be a linear, branched or cyclic alkyl or alkenylgroup, suitable groups containing up to 20 carbon atoms, preferably 1-12or 1-8 carbon atoms; in case of cyclic alkyl groups, R¹⁰ and R¹¹groupspreferably have at least 3 carbon atoms; preferably 3-12 or 3-8 carbonatoms. The groups may differ independently or be the same. Preferably,at least one of the R¹⁰ groups represents an ethyl group. In preferredembodiments, R¹⁰ and R¹¹ are ethyl, propyl or butyl: more preferably,all groups are ethyl groups. R¹⁰ and R¹¹ can also be aromatichydrocarbon groups, optionally substituted with e.g. alkyl groups andcan contain for example from 6 to 20 carbon atoms.

Preferably, M in said activating compound is Ti or Si. Preferably, thevalue of w is 0, the activating compound being for example a titaniumtetraalkoxide containing 4-32 C-atoms. The four alkoxide groups in thecompound may be the same or may differ independently. Preferably, atleast one of the alkoxy groups in the compound is an ethoxy group. Morepreferably the compound is a tetraalkoxide, like titanium tetraethoxide.Si-containing compounds suitable as activating compounds are the same aslisted above for step i).

Preferably, a TI-based compound, for example titanium tetraethoxide, isused together with an alcohol, like ethanol or methanol in step ii) togive the second intermediate reaction product.

If two or more compounds are used in step ii) of the preferred processaccording to the invention, their order of addition is not critical, butmay affect catalyst performance depending on the compounds used. Askilled person may optimize their addition based on some experiments.The compounds of step ii) can be added together or sequentially.

The first intermediate reaction product can be contacted in any sequencewith at least one activating compound selected from the group formed byelectron donors and compounds of formula) M(OR¹⁰)_(v-w)(OR¹¹)_(w) andM(OR¹⁰)_(v-w)(R¹¹)_(w). Preferably, the electron donor is first added tothe first intermediate reaction product and then the compound M(OR¹⁰)_(v-w)(OR¹¹)_(w) or M(OR¹⁰)_(v-w)(R¹¹)_(w) is added; in this order noagglomeration of solid particles is observed. The compounds in step ii)are preferably added slowly, for instance during a period of 0.1-6,preferably during 0.5-4 hours, most preferably during 1-2.5 hours, each.

The first intermediate reaction product and the electron donor and/orthe compound of formula M(OR¹⁰)_(v-w)(OR¹¹)_(w) orM(OR¹⁰)_(v-w)(R¹¹)_(w) may be contacted with an inert dispersant in stepii). The dispersant is preferably chosen such that virtually all sideproducts are dissolved in the dispersant and/or to act as an inertdiluent for the Mg-containing support particles. Any substance known inthe art that is inert to the Mg-containing support particles may be usedas inert dispersant. The dispersant may be an aromatic or aliphatichydrocarbon compound. The inert dispersant is preferably a hydrocarbonsolvent and more preferably it is selected from the groups of linear andbranched aliphatic and aromatic hydrocarbon compounds with, forinstance, 4-20 C-atoms. Suitable dispersants include for examplealiphatic and aromatic hydrocarbons and halogenated aromatic solventswith for instance 4-20 C-atoms; alkyl and aryl halides; ethers.Preferably, the dispersant is an aliphatic hydrocarbon, more preferablypentane, iso-pentane, hexane or heptane, heptane being most preferred.

The molar ratio of the activating compound to the magnesium atom of thefirst intermediate reaction product may range between wide limits andis, for instance, between 0.02 and 1.0. Preferably the molar ratio isbetween 0.1 and 0.7, depending on the type of activating compound, inthe process according to the invention, the temperature in step ii) canbe in the range from −20° C. to 70° C., preferably from −10° C. to 50°C., more preferably in the range between 0° C. and 30° C. Preferably, atleast one of the reaction components is dosed in time, for Instanceduring 0.1 to 6, preferably during 0.5 to 4 hours, more particularlyduring 1-2.5 hours.

The obtained second intermediate reaction product is typically a solidand may be further washed, preferably with the solvent also used asinert dispersant; and then stored and further used as a suspension insaid inert solvent. Alternatively, the product may be dried, preferablypartly dried, preferably slowly and under mild conditions; e.g. atambient temperature and pressure.

Starting from a solid Mg-containing product of controlled morphology,said morphology is not negatively affected during treatment with theactivating compound. The solid second intermediate reaction productobtained is considered to be an adduct of the Mg-containing compound andthe at least one compound as defined in step ii), and is still ofcontrolled morphology. This second intermediate reaction product can bealso referred herein as solid catalyst support containing magnesium.

Preferably, the solid first intermediate reaction product is contactedwith an alcohol and then with a titanium tetraalkoxide and optionally aninert dispersant to give a solid second intermediate reaction product,which is further applied in step iii).

Step iii)

Preferably, step iii) is carried out by contacting the secondintermediate reaction product with a halogen-containing Ti-compound anda monoester and then adding a 1,3-diether as an internal electron donor,and optionally, a diester as an additional internal electron donor, toprovide higher catalyst stereospecificity, high MFR and control thepolypropylene molecular structure.

An internal electron donor (also referred to as internal donor) isherein defined as an electron-donating compound that is commonlydescribed in prior art as a reactant in the preparation of a solidcatalyst component for a Ziegler-Natta catalyst system for an olefinpolymerization; i.e. contacting a magnesium-containing support with ahalogen-containing Ti compound and an internal donor.

The Ti/Mg molar ratio in the reaction between the second intermediatereaction product and halogen-containing titanium compound preferably isbetween 10 and 100, most preferably, between 10 and 50. Titaniumtetrachloride is the most preferred halogen-containing titaniumcompound.

The internal electron donor in step iii) (also referred herein as thefirst internal electron donor) can be any 1,3-diether known in the art,such as C6-C20 aromatic and C1-C20 aliphatic substituted 1,3-diethersand preferably, C10-C30, preferably C12-C20 polycyclic aromatichydrocarbons. Preferably, the 1,3-diether is2,2-diisobutyl-1,3-dimethoxypropane,2,2-dicyclopentyl-1,3-dimethoxypropane,2-ethyl-2-butyl-1,3-dimethoxypropane,2-isopropyl-2-isopentyl-1,3-dimethoxypropane,1,1-bis(methoxymethyl)-cyclopentadiene,1,1-bis(methoxyrnethyl)-2,3,4,5-tetramethylcyclopentadiene;1,1-bis(methoxyrnethyl)-2,3,4,5-tetraphenylcyclopentadiene;1,1-bis(methoxymethyl)indene;1,1-bis(methoxyrnethyl)-2,3-dimethylindene;1,1-bis(methoxyrnethyl)-cyclopenthylindene; 9,9-bis(methoxymethyi)fluorene; 9,9-bis(methoxymethyl)-2,3,6,7-tetrarnethylfluorene;9,9-bis(methoxymethyl)-2,3-benzofluorene;9,9-bis(methoxynnethyl)-2,7-dilsopropylfluorene;9,9-bis(methoxymethyl)-1,8-dichlorofluorene;9,9-bis(methoxymethyl)-2,7-dicyclopentylfluorene; 9,9-bis(methoxymethyl)difluorofluorene; 9,9-bis(methoxymethyl)-1,2,3,4-tertrahydrofluorene;and 9,9-bis(methoxymethyl)-4-tert-butylfluorene are used as an internalelectron donor. More preferably, the internal electron donor in stepiii) is selected from the group consisting of 1,3-diethers withfluorenyl ligand without or with substitutents having C1 to C10 carbonatoms for providing the higher hydrogen sensitivity. Most preferably,the internal electron donor is 9,9-bis-methoxymethyl-fluorene.

The molar ratio between the 1,3-diether and Mg may range from 0.03 to0.3, preferably from 0.04 to 0.2, and more preferably from 0.05 to 0.1.

The monoester according to the present invention can be any ester of amonocarboxylic acid known in the art. The monoester can have the formulaR′—CO—OR″, wherein R′ can be the same or different from R″.

R′ and R″ may be selected from the group consisting of hydrogen,straight, branched and cyclic alkyl having at most 20 carbon atoms andaromatic substituted and unsubstituted hydrocarbyl having 6 to 20 carbonatoms. Particularly, R′ may be selected from the group consisting ofhydrogen; straight and branched alkyl having 1 to 20 carbon atoms,preferably 1 to 10 carbon atoms and most preferably 1 to 5 carbon atoms;and cyclic alkyl having 3 to 20 carbon atoms, preferably 3 to 10 carbonatoms and most preferably 3 to 5 carbon atoms; and aromatic substitutedand unsubstituted hydrocarbyl having 6 to 20 carbon atoms, preferably 6to 10 carbon atoms.

Suitable examples of monoesters include formates, for instance, butylformate; acetates, for instance ethyl acetate, amyl acetate and butylacetate; acrylates, for instance ethyl acrylate, methyl methacrylate andisobutyl methacrylate; benzoates, particularly C1-C20 hydrocarbyl estersof benzoic acid, wherein the hydrocarbyl group is substituted orunsubstituted with one or more Group 14, 15 or 16 heteroatom containingsubstituents and C1-C20 (poly)hydrocarbyl ether derivatives thereof,preferably, C1-C4 alkyl benzoate and C1-C4 ring alkylated derivativesthereof; more preferably, methyl benzoate, ethyl benzoate, propylbenzoate, methyl p-methoxy benzoate, methyl p-ethoxy benzoate; mostpreferably ethyl benzoate. Other suitable examples includemethyl-p-toluate and ethyl-naphthate. More preferably, the monoester isan acetate or a benzoate. Most preferably, the monoester is ethylacetate, amyl acetate or ethyl benzoate,

Most preferably, the monoester used in step iii) is an ester of analiphatic rnonocarboxylic acid having C1-C10 carbon atoms.

The molar ratio between the monoester in step iii) and Mg may range from0.05 to 0.5, preferably from 0.1 to 0.4, and most preferably from 0.15to 0.25.

In an embodiment, the amount of monoester is less than 4 wt. % based onthe total weight of the catalyst component, preferably the amount ofmonoester is at most 3.5 wt. %. In an embodiment, the amount ofmonoester is at least 2.5 wt. %. This amount is sufficiently low toensure that the monoester will only react as activator and (hardly) notas internal donor, The effect on the selectivity of the 1,3-diether asinternal donor is hence remained without any significant effect of themonoester also acting as internal donor.

The monoester in step iii) of the present invention is not astereospecificity agent, like usual internal donors are known to be inthe prior art. Without to be bound by any theory, the inventors believethat the monoester used in the process according to the presentinvention participates at the formation of the magnesium halogen (e.g.MgCl₂) crystallites during the Interaction of Mg-containing support withtitanium halogen (e.g. TiCl₄). The monoester may form intermediatecomplexes with Ti and Mg halogen compounds (for instance, TiCl₄,TiCl₃(OR), MgCl₂, MgCl(OEt), etc.), help to the removal of titaniumproducts from solid particles to mother liquor and affect the activityof final catalyst. Therefore, the monoester according to the presentinvention can also be referred to as an activating agent.

The diester (also referred herein as the second internal electron donor)can be any diester of a C6-C20 aromatic and C1-C20 aliphaticdicarboxylic acid known in the art. Suitable examples of diestersinclude C6-C20 aromatic or a C1-C20 aliphatic substituted phthalates,e.g. dibutyl phthalate, diisobutyl phthalate, diallyl phthalate and/ordiphenyl phthalate; C6-C20 aromatic or a C1-C20 aliphatic substitutedsuccinates; and also C6-C20 aromatic or a C1-C20 aliphatic substitutedesters of malonic acid or glutaric acid. Preferably the diester is aC1-010 aliphatic substituted phthalate, more preferably dibutylphthalate.

The molar ratio between the diester of step iii) and Mg may range from0.03 to 0.15, preferably from 0.05 to 0.1.

The second intermediate reaction product can be contacted with thehalogen-containing Ti-compound, the monoester, the 1,3-diether andoptionally the diester at any time and any stage and by applying anymethod known to the skilled person in the art.

Preferably, at first the second intermediate reaction product iscontacted with the halogen-containing Ti-compound and then the monoesteris added to the reaction (may be also referred herein as stage I oftitanation reaction) and then the 1,3-diether is added to the reaction(may be also referred herein as stage II or III of titanation reaction)and then optionally the diester is added to the reaction.

Particularly, in step iii) the second intermediate reaction product maybe contacted with titanium tetrachloride and the monoester at a reactiontemperature that may be between 80° C. and 130° C., preferably 90 and120° C. and a reaction time that may be 50 to 150 min, preferably for 90to 110 min (stage I of reaction). After a purification step (such asseparation and washing), a halogen-containing titanium compound may beadded to the product of stage I and the reaction may be kept at atemperature of between 80 and 120° C. for preferably 20 to 60 min (stageII of reaction). Stage II may be repeated once (stage III of reaction).The 1,3-diether may be added after the monoester and preferably, the1,3-diether is added in stage III or I when the diester is not added orin stage II when the diester is added. The diester is more preferablyadded in stage III of the reaction. Chlorobenzene may be used as theeffective solvent for the removal of titanation products (e.g,TiCl_(n)(OEt)_(4-n)) and their complexes with donors from solidparticles to mother liquor.

The reaction temperature during contacting in step iii) the secondintermediate reaction product and the halogen-containing titaniumcompound may be preferably between 0° C. and 150° C., more preferablybetween 50° C. and 150° C., and more preferably between 80° C. and 130°C. Most preferably, the reaction temperature is between 90° C. and 120°C. The contacting time between the components in step iii) may bebetween 10 and 200 min, preferably between 30 and 120 min. During thetitanation reaction an inert aliphatic or aromatic hydrocarbon orhalogenated aromatic compound can be used. If desired, the reaction andsubsequent purification steps may be repeated one or more times. A finalwashing is preferably performed with an aliphatic hydrocarbon to resultin a suspended or at least partly dried catalyst component, as describedabove for the other steps.

The invention further relates to a catalyst component for polymerizationof an olefin obtainable by the process according to the invention. Thiscatalyst component comprises Ti, Mg, a halogen, a monoester, a1,3-diether as an internal electron donor, and optionally a diester asan additional internal electron donor. Particularly, said catalystcomponent comprises a magnesium-containing support, a halogen-containingtitanium compound, a monoester as activating agent, a 1,3-diether as aninternal electron donor, and optionally a diester as an additionalinternal electron donor. All these components are as defined herein.More preferably, the catalyst component according to the presentinvention comprises a magnesium dichloride, titanium tetrachloride, amonoester as activating agent, a 1,3-diether and optionally a diester asinternal electron donors. By applying said catalyst obtainable with theprocess, higher MFRs and high isotacticity of the polyolefins areobtained.

The invention also relates to the use of the monoester as activatingagent in a catalyst component for polymerization of an olefin.

The term “catalyst component” may be also referred herein to as“procatalyst” or “solid catalyst component” or “catalyst precursor”.

The invention also relates to a catalyst system for polymerization of anolefin that comprises the catalyst component according to the inventionand a co-catalyst. Preferably, the catalyst system also comprises anexternal electron-donating compound, also referred to as externalelectron donor, or simply external donor. The main function of thisexternal donor compound is to affect the stereoselectivity of thecatalyst system in polymerization of an olefin having 3 or more carbonatoms, and therefore it may be also referred to as selectivity controlagent.

The invention further relates to a process of making a polyolefin bycontacting at least one olefin with a polymerization catalyst systemcomprising the catalyst component according to the present invention.

Preferably, the polyolefin made by using the catalyst system of thepresent invention is polypropylene. It is an advantage of the presentinvention that polypropylene obtainable by employing said catalyst hashigher MFR, low atactic polymer fraction and high isotacticity.

The preparation of polyolefins may take place by polymerizing an olefin,i.e. one or more olefins simultaneously and/or successively in thepresence of a catalyst system comprising the catalyst componentobtainable by the process according to the invention, a co-catalyst andoptionally an external donor. The olefin according to the invention maybe selected from mono- and di-olefins containing from 2 to 10 carbonatoms, such as for example ethylene, propylene, butylene, hexene, octeneand/or butadiene. According to a preferred embodiment of the inventionthe olefin is propylene or a mixture of propylene and ethylene, toresult in a propylene homopolymer or copolymer. The present inventionincludes in one aspect a polyolefin obtained or obtainable by a processfor making a polyolefin according to the present invention, preferablysaid polyolefin is a polypropylene, more preferably a homopolymer ofpropylene. A propylene copolymer is herein meant to include bothso-called random copolymers with relatively low comonomer content, e.g.up to 10 mol %, as well as so-called impact, also known as heterophasicor block propylene copolymers comprising higher comonomer contents, e.g.from 5 to 80 mol %, more typically from 10 to 60 mol %. The impactcopolymers are actually blends of different propylene polymers; suchcopolymers can be made in one or two reactors and can be blends of afirst component of low comonomer content and high crystallinity, and asecond component of high comonomer content having low crystallinity oreven rubbery properties. Such random and impact copolymers arewell-known to the skilled person in the art.

Preferably, the co-catalyst is an organometallic compound containing ametal from group 1, 2, 12 or 13 of the Periodic System of the Elements(Handbook of Chemistry and Physics, 70th Edition, CRC Press, 1989-1990),wherein the system further comprises an external electron donor.Preferably, the co-catalyst is an organoalumlnium compound. Theorganoaluminium compound may be, for instance, a compound having theformula AIR¹⁵ ₃, wherein each R¹⁵ independently represents an alkylgroup with, for instance, 1-10 C-atoms or an aryl group with, forinstance, 6-20 C-atoms. Examples of a suitable organoaluminium compoundare trimethylaluminium, triethylaluminium, trilsobutylaiuminium, and/ortrioctylaiuminium. Preferably, the co-catalyst is triethylalumlnium.

The molar ratio of the metal of the co-catalyst relative to titanium inthe polymerization catalyst system during the polymerization may varyfor instance from 5 to 2000. Preferably, this ratio is between 50 and300.

Examples of suitable external donors include organo-silicon compounds.Mixtures of external donors can also be used. Examples of organo-siliconcompounds that are suitable as external donor are compounds or mixturesof compounds of general formula Si(OR¹⁶)_(4-n)R¹⁷ _(n), wherein n can hefrom 0 up to 2 preferably n is 1 or 2 as higher values have no positiveeffect on stereospecificity, and each R¹⁶ and R¹⁷, independently,represents an alkyl or aryl group, optionally containing one or morehetero atoms for instance O, N, S or P, with, for instance, 1-20C-atoms, as defined above for R¹³ and R¹⁴. Examples of suitablecompounds include the silane-compounds that can be used at step i), asdescribed above. Preferably the organo-silicon compound used as externaldonor is n-propyl trimethoxysilane.

The aluminium/external donor molar ratio in the polymerization catalystsystem preferably is between 1 (if less than 1 no polymerization occurs)and 200; more preferably between 5 and 100.

Preferably, no external donor is used in said catalyst system aspolymers having high I1AFR (e.g. higher than 20 dg/min or higher than 40dg/min or even higher than 50 dg/min) and also low amount of atacticpolymers and relatively low XS are obtained. It is an additionaleconomic advantage of the present invention that the use of an externaldonor can be avoided.

The polymerization process can be carried out in the gas phase or in theliquid phase (in bulk or slurry). In the case of polymerization in aslurry (liquid phase) a diluent may be present. Suitable diluentsinclude for example n-butane, isobutane, n-pentane, isopentane, hexane,heptane, octane, cyclohexane, benzene, toluene, xylene and liquidpropylene. The polymerization conditions of the process according to theinvention, such as for example the polymerization temperature and time,monomer pressure, avoidance of contamination of catalyst, choice ofpolymerization medium in slurry processes, the use of furtheringredients (like hydrogen) to control polymer molar mass, and otherconditions are well known to persons of skill in the art. Thepolymerization temperature may vary within wide limits and is, forexample for propylene polymerization, between 0° C. and 120° C.,preferably between 40° C. and 100° C. The pressure during (propylene)(co)polymerization is for instance between 0.1 and 6 MPa, preferablybetween 0.5-3 MPa.

The molar mass of the polyolefin obtained during the polymerization canbe controlled by adding during the polymerization hydrogen or any otheragent known to be suitable for the purpose. The polymerization can becarried out in a continuous mode or batch-wise. Slurry-, bulk-, andgas-phase polymerization processes, multistage processes of each ofthese types of polymerization processes, or combinations of thedifferent types of polymerization processes in a multistage process arecontemplated herein. Preferably the polymerization process is a singlestage gas phase process or a multistage, for instance a 2-stage, gasphase process wherein in each stage a gas-phase process is used.

Examples of gas-phase polymerization processes include both stirred bedreactors and fluidized bed reactor systems; such processes are wellknown in the art. Typical gas phase α-olefin polymerization reactorsystems comprise a reactor vessel to which alpha-olefin monomer(s) and acatalyst system can be added and which contain an agitated bed ofgrowing polymer particles.

The present invention further relates to the use of the catalystcomponent obtainable by the process according to the present inventionfor polymerization of an olefin. Polyolefins with high MFR, highisotacticity and low amount of atactic polymer fraction are produced byusing said catalyst.

It is noted that the invention relates to all possible combinations offeatures recited in the claims. Features described in the descriptionmay further be combined.

Although the invention has been described in detail for purposes ofillustration, it is understood that such detail is solely for thatpurpose and variations can be made therein by those skilled in the artwithout departing from the spirit and scope of the invention as definedin the claims.

It is further noted that the invention relates to all possiblecombinations of features described herein, preferred in particular arethose combinations of features that are present in the claims.

It is further noted that the term ‘comprising’ does not exclude thepresence of other elements. However, it is also to be understood that adescription on a product comprising certain components also discloses aproduct consisting of these components. Similarly, it is also to beunderstood that a description on a process comprising certain steps alsodiscloses a process consisting of these steps.

The invention will be further elucidated with the following exampleswithout being limited hereto.

EXAMPLES Example 1

A. Grignard Formation Step

This step was carried out as described in Example XVI of EP 1 222 214B1.

A stainless steel reactor of 9 I volume was filled with magnesium powder360 g. The reactor was brought under nitrogen. The magnesium was heatedat 80° C. for 1 hour, after which a mixture of dibutyl ether (1 liter)and chlorobenzene (200 ml) was added, Then iodine (0.5 g) andn-chlorobutane (50 ml) were successively added to the reaction mixture.After the colour of the iodine had disappeared, the temperature wasraised to 94° C. Then a mixture of dibutyl ether (1.6 liter) andchlorobenzene (400 ml) was slowly added for 1 hour, and then 4 liter ofchlorobenzene was slowly added for 2.0 hours. The temperature ofreaction mixture was kept in Interval 98-105° C. The reaction mixturewas stirred for another 6 hours at 97-102° C. Then the stirring andheating were stopped and the solid material was allowed to settle for 48hours. By decanting the solution above the precipitate, a solution ofphenylmagnesiumchloride reaction product A has been obtained with aconcentration of 1.3 mol Mg/l. This solution was used in the furthercatalyst preparation.

B. Preparation of the First Intermediate Reaction Product

This step was carried out as described in Example XX of EP 1 222 214 B1,except that the dosing temperature of the reactor was 35° C., the dosingtime was 360 min and the propeller stirrer was used. 250 ml of dibutylether was introduced to a 1 liter reactor. The reactor was fitted bypropeller stirrer and two baffles. The reactor was thermostated at 35°C.

The solution of reaction product of step A (360 ml, 0.488 mol Mg) and180 ml of a solution of tetraethoxysilane (TES) in dibutyl ether (DBE),(55 ml of TES and 125 ml of DBE), were cooled to 10° C., and then weredosed simultaneously to a mixing device of 0.45 ml volume supplied witha stirrer and jacket. Dosing time was 360 min. Thereafter the premixedreaction product A and the TES-solution were introduced to a reactor.The mixing device (minimixer) was cooled to 10° C. by means of coldwater circulating in the minimixer's jacket. The stirring speed in theminimixer was 1000 rpm. The stirring speed in reactor was 350 rpm at thebeginning of dosing and was gradually increased up to 600 rpm at the endof dosing stage.

On the dosing completion the reaction mixture was heated up to 60° C.and kept at this temperature for 1 hour. Then the stirring was stoppedand the solid substance was allowed to settle. The supernatant wasremoved by decanting. The solid substance was washed three times using500 ml of heptane. As a result, a pale yellow solid substance, reactionproduct B (the solid first intermediate reaction product; the support),was obtained, suspended in 200 ml of heptane. The average particle sizeof support was 22 μm and span value (d₉₀-d₁₀)/d₅₀=0.5.

C. Preparation of the Second Intermediate Reaction Product

Support activation was carried out as described in Example VIII of EP2027164B1 to obtain the second intermediate reaction product.

In inert nitrogen atmosphere at 20° C. a 250 ml glass flask equippedwith a mechanical agitator is filled with slurry of 5 g of reactionproduct B dispersed in 60 ml of heptane. Subsequently a solution of 0.22ml ethanol (EtOH/Mg=0.1) in 20 ml heptane is dosed under stirring during1 hour. After keeping the reaction mixture at 20° C. for 30 minutes, asolution of 0.79 ml titanium tetraethoxide (TET/Mg=0.1) in 20 ml ofheptane was added for 1 hour.

The slurry was slowly allowed to warm up to 30° C. for 90 min and keptat that temperature for another 2 hours. Finally the supernatant liquidis decanted from the solid reaction product (the second intermediatereaction product; activated support) which was washed once with 90 ml ofheptane at 30° C.

D. Preparation of the Catalyst Component

A reactor was brought under nitrogen and 125 ml of titaniumtetrachloride was added to it. The reactor was heated to 90° C. and asuspension, containing about 5.5 g of activated support in 15 ml ofheptane, was added to it under stirring. The reaction mixture was keptat 90° C. for 10 min. Then add 0.866 g of ethyl acetate (EA/Mg=0.25molar ratio). The reaction mixture was kept for 60 min (stage I ofcatalyst preparation). Then the stirring was stopped and the solidsubstance was allowed to settle. The supernatant was removed bydecanting, after which the solid product was washed with chlorobenzene(125 ml) at 90° C. for 20 min. The washing solution was removed bydecanting, after which a mixture of titanium tetrachloride (62.5 ml) andchlorobenzene (62.5 ml) was added. The reaction mixture was kept at 90°C. for 30 min (stage II of catalyst preparation). After which thestirring was stopped and the solid substance was allowed to settle. Thesupernatant was removed by decanting, after which a mixture of titaniumtetrachloride (62.5 ml) and chlorobenzene (62.5 ml) was added. Then 0.5g of 9,9-bis-methoxymethyl-fluorene (flu) (flu/Mg=0.05 molar ratio) in 3ml of chlorobenzene was added to reactor and the temperature of reactionmixture was increased to 115° C. The reaction mixture was kept at 115°C. for 30 min (stage III of catalyst preparation). After which thestirring was stopped and the solid substance was allowed to settle. Thesupernatant was removed by decanting, after which a mixture of titaniumtetrachloride (62.5 ml) and chlorobenzene (62.5 ml) was added. Thereaction mixture was kept at 115° C. for 30 min (stage IV of catalystpreparation), after which the solid substance was allowed to settle. Thesupernatant was removed by decanting and the solid was washed five timesusing 150 ml of heptane at 60° C., after which the catalyst component,suspended in heptane, was obtained.

E. Polymerization of Propylene

Polymerization of propylene was carried out in a stainless steel reactor(with a volume of 0.7 I) in heptane (300 ml) at a temperature of 70° C.,total pressure 0.7 MPa and hydrogen presence (55 ml) for 1 hour in thepresence of a catalyst system comprising the catalyst componentaccording to step D, triethylaluminlum and n-propyltrlmethoxysilane. Theconcentration of the catalyst component was 0.033 g/l; the concentrationof triethyialuminium was 4.0 mmol/l; the concentration ofn-propyltrimethoxysilane was 0.2 mmol/l.

Data on the catalyst performance at the propylene polymerization arepresented in Table 1. In Table 1 herein, “ME” means monoester.

Example 1a

Example 1a was carried out in the same way as Example 1, but in step Eno n-propyitrimethoxysilane was used.

Example 2

Grignard Formation Step

A stirred flask, fitted with a reflux condenser and a funnel, was filledwith magnesium powder (24.3 g). The flask was brought under nitrogen.The magnesium was heated at 80° C. for 1 hour, after which dibutyl ether(150 ml), iodine (0.03 g) and n-chlorobutane (4 ml) were successivelyadded. After the colour of the iodine had disappeared, the temperaturewas raised to 80° C. and a mixture of n-chlorobutane (110 ml) anddibutyl ether (750 ml) was slowly added for 2.5 hours. The reactionmixture was stirred for another 3 hours at 80° C. Then the stirring andheating were stopped and the small amount of solid material was allowedto settle for 24 hours. By decanting the colorless solution above theprecipitate, a solution of butylmagnesiumchloride (reaction product ofstep A) with a concentration of 1.0 mol Mg/l was obtained.

B. Preparation of the First Intermediate Reaction Product

This step was carried out as step B described in Example 1, except thatthe solution of reaction product of step A of Example 2 (360 ml, 0.36mol Mg) and 180 ml of a solution of tetmethoxysilane (TES) in dibutylether (38 ml of TES and 142 ml of DBE), were used. As a result, a whitesolid reaction product of step B (the first intermediate reactionproduct; the support), was obtained, suspended in 200 ml of heptane. Theaverage particle size of support was 20 μm and span value(d₉₀-d₁₀)/d₅₀=0.65.

C. Preparation of the Second Intermediate Reaction Product

In inert nitrogen atmosphere at 20° C. a 250 ml glass flask equippedwith a mechanical agitator is filled with slurry of 5 g of the firstintermediate reaction product (see above step B of Example 2) dispersedin 60 ml of heptane. Subsequently a solution of 0.86 ml methanol(MeOH/Mg=0.5 mol) in 20 ml heptane is dosed under stirring during 1hour. After keeping the reaction mixture at 20° C. for 30 minutes theslurry was slowly allowed to warm up to 30° C. for 30 min and kept atthat temperature for another 2 hours. Finally the supernatant liquid isdecanted from the solid reaction product (the second intermediatereaction product; activated support) which was washed once with 90 ml ofheptane at 30° C.

D. Preparation of the Catalyst Component

This step was carried out as step D described in Example 1, except that5.3 g of the above activated support, 0.937 g of ethyl acetate(EA/Mg=0.25 molar ratio) and 0.541 g of 9,9-bis-methoxymethyl-fluorene(flu/Mg=0.05 molar ratio) were used.

E. Polymerization of Propylene

This step was carried out as step E described in Example 1.

Example 2a

Example 2a was carried out in the same way as Example 2, but in step Eno n-propyltrimethoxysilane was used.

Example 3

Example 3 was carried out in the same way as Example 2, but flu/Mg=0.1molar ratio was used in step D instead of flu/Mg=0.05 molar ratio.

Example 3a

Example 3a was carried out in the same way as Example 3, but in step Eno n-propyltrimethoxysilane was used.

Example 4

Example 4 was carried out in the same way as Example 3, butethylbenzoate (EB/Mg=0.15 molar ratio) and 100° C. at stages I and IIwere used in step D instead of EA/Mg=0.25 molar ratio and 90° C.

Example 4a

Example 4a was carried out in the same way as Example 4, but in step Eno n-propyltrimethoxysilane was used.

Example 5

Example 5 was carried out in the same way as Example 2, but thepreparation of the catalyst component in step D was performed asfollows.

A reactor was brought under nitrogen and 62.5 ml of titaniumtetrachloride was added to it. The reactor was heated to 90° C. and asuspension, containing about 5.3 g of activated support in 15 ml ofheptane, was added to it under stirring. Then the reaction mixture waskept at 90° C. for 10 min, and 0.937 g of ethyl benzoate (EA/Mg=0.25molar ratio) in 2 ml of chlorobenzene was added to reactor. The reactionmixture was kept at 90° C. for 10 min, and 62.5 ml of chlorobenzene wasadded to reactor. The reaction mixture was kept at 90° C. for 30 min,and 1.082 g of 9,9-bis-methoxymethyl-fluorene (flu/Mg=0.1 molar ratio)in 3 ml of chlorobenzene was added to reactor. Temperature of reactionmixture was increased to 115° C. and the reaction mixture was kept at115° C. for 60 min (stage I of catalyst preparation). Then the stirringwas stopped and the solid substance was allowed to settle. Thesupernatant was removed by decanting, after which the solid product waswashed with chlorobenzene (125 ml) at 100-110° C. for 20 min. Then thewashing solution was removed by decanting, after which a mixture oftitanium tetrachloride (62.5 ml) and chlorobenzene (62.5 ml) was added.The reaction mixture was kept at 115° C. for 30 min (stage II ofcatalyst preparation), after which the solid substance was allowed tosettle. The supernatant was removed by decanting, and the last treatmentwas repeated once again (stage III of catalyst preparation). The solidsubstance obtained was washed five times using 150 ml of heptane at 60°C., after which the catalyst component, suspended in heptane, wasobtained.

Example 5a

Example 5a was carried out in the same way as Example 5, but in step Eno n-propyltrimethoxysilane was used.

Example 6

Example 6 was carried out in the same way as Example 5, but in step Dethylbenzoate (EB/Mg=0.15 molar ratio) at 100° C. instead of EA wasused.

Example 6a

Example 6a was carried out in the same way as Example 6, but in step Eno n-propyltrimethoxysilane was used.

Example CE1 (comparative experiment 1)

Example CE1 was carried out in the same way as Example 1, but thepreparation of the catalyst component in step D was performed asfollows.

A reactor was brought under nitrogen and 125 ml of titaniumtetrachloride was added to it. The reactor was heated to 100° C. and asuspension, containing about 5.5 g of activated support in 15 ml ofheptane, was added to it under stirring. Then the temperature ofreaction mixture was increased to 110° C. for 10 min and 1.5 g of9,9-bis-methoxyrnethyl-fluorene (flu) (flu/Mg=0.15 molar ratio) in 3 mlof chlorobenzene was added to reactor. Temperature of reaction mixturewas increased to 115° C. and the reaction mixture was kept at 115° C.for 105 min (stage I of catalyst preparation). Then the stirring wasstopped and the solid substance was allowed to settle. The supernatantwas removed by decanting, after which the solid product was washed withchlorobenzene (125 ml) at 100-110° C. for 20 min. Then the washingsolution was removed by decanting, after which a mixture of titaniumtetrachloride (62.5 ml) and chlorobenzene (62.5 ml) was added. Thereaction mixture was kept at 115° C. for 30 min (stage II of catalystpreparation), after which the solid substance was allowed to settle. Thesupernatant was removed,by decanting, and the last treatment wasrepeated once again (stage III of catalyst preparation). The solidsubstance obtained was washed five times using 150 ml of heptane at 60°C., after which the catalyst component, suspended in heptane, wasobtained.

Example CE1a (comparative experiment 1a)

Example CE1a was carried out in the same way as Example CE1, but in stepE no n-propyltrimethoxysilane was used.

Example CE2 (comparative experiment 2)

Example CE2 was carried out in the same way as Example CE1, butEA/Mg=0.25 molar ratio and 90° C. was used in step ID at I stage insteadof flu/Mg=0.16 molar ratio and 115° C.

Example CE3 (comparative experiment 3)

Example CE3 was carried out in the same way as Example 2, but step D wasperformed without monoester at same conditions as in Example CE1(flu/Mg=0.15 molar ratio).

Example CE3a (comparative experiment 3a)

Example CE3a was carried out in the same way as Example CE3, but in stepE no n-propyltrirnethoxysilane was used.

Example CE4 (comparative experiment 4)

Example CE4 was carried out in the same way as Example CE1, butEB/Mg=0.15 molar ratio and 100° C. were used in step D at stage Iinstead of flu/Mg=0.16 molar ratio and 115° C.

Example 6

Example 6 was carried out in the same way as Example 2, but stage II instep D was performed with flu/Mg=0.04 mol at 115° C.,di-n-butylphthalate (DBP) at DBP/Mg=4.1 molar ratio was used in stageIII.

Example 6a

Example 6a was carried out in the same way as Example 6, but in step Eno n-propyltrimethoxysi lane was used.

Example CE5 (comparative experiment 5)

Example CE5 was carried out in the same way as Example VIII of EP2027164B1 under conditions of Example CE1, but in step Ddi-n-butylphthalate (DBP) as in EP2027164B1 was used at DBP/Mg=0.15molar ratio instead of flu/Mg=0.15 molar ratio.

Example 7

Example 7 was carried out in the same way as Example, but in step Dstage I was performed with EA/Mg=0.15 molar ratio, stage II wasperformed with flu/Mg=0.04 mol at 115° C., and stage III withdi-n-butylphthalate (DBP) at DBP/Mg=0.05 molar ratio.

Example 7a

Example 7a was carried out in the same way as Example 7, but in step Eno n-propyltrimethoxysilane was used.

Example 8

Example 8 was carried out in the same way as Example 7, but EB/Mg=0.15molar ratio at 100° C. and flu/Mg=0.03 molar ratio were used in step Dinstead of EA/Mg=0.15 and flu/Mg=0.04 molar ratios respectively.

Example 8a

Example 8a was carried out in the same way as Example 8, but in step Eno n-propyltrirnethoxysilane was used.

Example 9

Example 9 was carried out in the same way as Example 8, but flu/Mg=0.04and DBP/Mg=0.1 molar ratios were used in step D instead of flu/Mg=0.03and DBP/Mg=0.05 molar ratios.

Example 9a

Example 9a was carried out in the same way as Example 9, but in step Eno n-propyltrimethoxysilane was used.

TABLE 1 1,3- PP yield, 1,3- diether, ME Ti, kg/g APP, XS, MFR, Ex.diether/Mg ME/Mg wt % Wt % wt % cat. wt % % dg/min Mw/Mn 1 0.05 0.2513.7 3.3 2.9 12.0 0.53 3.0 13.3 3.8 (EA) 1a 0.05 0.25 13.7 3.3 2.9 19.40.78 5.8 40.3 4.3 (EA) 2 0.05 0.25 9.7 n.d. 3.2 8.7 0.43 4.6 18.1 5.6(EA) 2a 0.05 0.25 9.7 n.d. 3.2 15.3 3.2 10.9 45.8 4.9 (EA) 3 0.1 0.2512.0 n.d. 2.7 6.4 0.6 3.8 20.2 5.9 (EA) 3a 0.1 0.25 12.0 n.d. 2.7 11.01.0 7.0 30.0 5.1 (EA) 4 0.1 0.15 11.8 3.6 2.8 5.4 0.9 4.6 15.6 5.9 (EB)4a 0.1 0.15 11.8 3.6 2.8 7.3 1.0 7.3 32.2 5.2 (EB) 5 0.1 0.25 7.6 n.d.3.1 7.2 1.0 6.4 17.6 5.6 (EA) 5a 0.1 0.25 7.6 n.d. 3.1 12.1 4.0 10.548.3 5.0 (EA) 6 0.1 0.15 8.9 2.7 2.9 9.1 1.0 6.0 19.2 5.7 (EB) 6a 0.10.15 8.9 2.7 2.9 17.4 3.1 11.0 57.7 5.1 (EB) CE1 0.15 0 16.5 0 3.4 9.20.8 3.5 10.7 5.1 CE1a 0.15 0 16.5 0 3.4 13.6 1.2 4.3 21.8 4.6 CE2 0 0.250 n.d. 3.8 5.3 7.3 10.8 19.2 5.1 (EA) CE3 0.15 0 12.7 0 2.8 4.2 1.0 4.58.7 6.2 CE3a 0.15 0 12.7 0 2.8 6.3 1.3 7.1 12.4 5.3 CE4 0 0.15 0 n.d.2.6 5.3 7.1 12.0 22.6 5.8 (EB)

TABLE 2 PP 1,3- 1,3- yield diether/ diether ME DAP Ti kg/g APP XS MFREx. Mg DBP/Mg ME/Mg wt % Wt. % wt % wt % cat wt % % dg/min Mw/Mn 7 0.030.05 0.15 5.5 n.d. 7.8 2.9 9.4 0.57 3.4 14.5 4.8 (EA) 7a 0.03 0.05 0.155.5 n.d. 7.8 2.9 10.7 1.9 0.2 43.9 4.9 (EA) 8 0.03 0.05 0.15 5.2 1.3 7.62.3 11.0 0.52 3.6 16.2 4.4 (EB) 8a 0.03 0.05 0.15 5.2 1.3 7.6 2.3 12.52.5 5.3 46.1 4.3 (EB) 9 0.04 0.1 0.15 5.8 0.8 9.5 2.0 9.7 0.4 2.0 14.64.6 (EB) 9a 0.04 0.1 0.15 5.8 0.8 9.5 2.0 10.5 1.7 8.9 52.8 4.3 (EB) CE50 0.15 0 0 0 10.5 2.6 13.5 0.5 3.0 12.7 4.8

Abbreviations and Measuring Methods:

-   -   PP yield, kg/g cat is the amount of polypropylene obtained per        gram of catalyst component.    -   APP, wt % is the weight percentage of atactic polypropylene.        Atactic PP is the PP fraction soluble in heptane during        polymerization. APP was determined as follows: 100 ml of the        filtrate (y ml) obtained in separating the polypropylene powder        (x g) and the heptane was dried over a steam bath and then under        vacuum at 60° C. That yielded z g of atactic PP. The total        amount of Atactic PP (q g) is: (y/100)*z. The weight percentage        of Atactic PP is: (q/(q+x))*100%.    -   XS, wt % is xylene solubles, measured according to ASTM D        5492-10.    -   MFR is the melt flow rate as measured at 230° C. with 2.16 kg        load, measured according to ISO 1133.    -   Mw/Mn: Polymer molecular weight and its distribution (MWD) were        determined by Waters 150C gel permeation chromatograph combined        with a Viscotek 100 differential viscosimeter. The chromatograms        were run at 140° C. using 1,2,4-trichlorobenzene as a solvent        with a flow rate of 1 ml/min. The refractive index detector was        used to collect the signal for molecular weights.

Conclusions from the Experimental Data:

In order to determine the effect of the combination of a monoesteractivator and a 1,3-diether internal donor, Example 1 can be compared toComparative Example 1; Example 1a can be compared to Comparative Example1a; Examples 2 and 3 can be compared to Comparative Example 3 andExamples 2a and 3a can be compared to Comparative Example 3a.

Ex. 1 compared to Ex. CE1 (no monoester) shows an increase of hydrogensensitivity because the MFR values are higher by 24% (from 10.7 to 13.3dg/min). Also an increase of catalyst activity is observed (from 9.2 to12.0 kg PP yield per gram of catalyst) and it was observed that lessinternal donor was required, viz. 3 times lower amount of used1,3-diether.

Ex. 1a compared to Ex. CE1a (no monoester) shows an increase of hydrogensensitivity because the MFR values are higher by 85% (from 21.8 to 40.3dg/min). Also an increase of catalyst activity is observed (from 13.5 to19.4 kg PP yield per gram of catalyst) and it was observed that lessinternal donor was required, viz. 3 times lower amount of used1,3-diether. Ex. 2 and 3 compared to Ex. CE3 (no monoester) show: I) anincrease of hydrogen sensitivity because the MFR values are higher by2.1 (Ex.2) or even2.3 (Ex. 3) times ; ii) an significant increase ofcatalyst activity from 4.2 to 8.7 (Ex.2) or 6.4 (Ex.3) ; ill) a loweramount (in 2-3 times) of used 1,3-diether (from 0.15 to 0.05 (Ex.2) or0.1 (Ex.3).

Ex. 2a and 3a compared to Ex. CE3a (no monoester) show: I) an increaseof hydrogen sensitivity because the MFR values are higher by 2.4 (Ex.2a)or even 3.7 (Ex.3a) times; ii) an significant increase of catalystactivity from 6.3 to 15.3 (Ex.2) or 11.0 (Ex.3); iii) a lower amount (in2-3 times) of used 1,3-diether(from 0.15 to 0.05 (Ex.2) or 0.1 (Ex. 3).

In order to determine the effect of the combination of a monoester and a1,3-diether internal donor also comparative tests (Comparative Examples2 and 4) have been done wherein no 1,3-diether internal donor ispresent. Example 3 can be compared to Comparative Example 2; Example 4can be compared to Comparative Example 4.

Ex. 3 compared to Ex. CE2 (no 1,3-diether) show: an increase in yieldfrom 5.3 to 6.4, a significant decrease in XS wt. % from 10.8 to 3.8 anda significant decrease in APP wt. % from 7.3 to 0.6.

Ex. 4 compared to Ex. CE4 (no 1,3-diether) show: a similar yield 5.3 and5.4, a significant decrease in XS wt. % from 12.0 to 4.6 and asignificant decrease in APP wt. % from 7.1 to 0.9.

In order to determine the effect of the type of monoester Example 4using ethylbenzoate as monoester can be compared to Example 3 usingethylacetate as monoester

Ex. 4 (EB as monoester) compared to Ex. 3 (EA as monoester) showssimilar hydrogen sensitivity and APP/XS values at lower catalystactivity;

In order to determine the effect of the moment of addition of the1,3-diether with respect to the monoester Examples 5 and 6 can becompared to Example 3.

Ex. 5 and Ex. 6 (EB as monoester) are performed as Ex. 3 but 1,3-dietheris introduced after monoester at stage I instead of stage III. Ex. 5 andEx. 6 show that hydrogen sensitivity and catalyst activity are higherthan that in Ex. CE3 (no monoester) and similar or higher to that in Ex.3.

In order to determine the effect of the presence of an additionalinternal donors Examples 7-9 have been carried out.

Ex. 7-9 are performed using EA or EB as monoester and two internaldonors (1,3-diether and DBP) and show high hydrogen sensitivity which issimilar or higher to that in Ex. 1 (using EA and 1,3-diether) andsignificantly higher than that in Ex. CE1 (using only 1,3-dietherwithout monoester) or Ex. CE5 (using only DBP).

From the above examples it can thus be concluded that the key to thepresent invention is the very specific combination of a monoester—asactivator—and a 1,3-diether(e.g. a fluorene) as internal donor. Thisinventive combination of activator and internal donor leads to a higheryield and a higher melt flow rate, while the molecular weightdistribution remains the same or even improves.

1-9. (canceled)
 10. A catalyst component manufactured by a processcomprising: contacting a compound R⁹ _(z),MgX_(2-z) wherein R⁹ is anaromatic, aliphatic or cyclo-aliphatic group containing up to 20 carbonatoms, X is a halide, and z is in a range of larger than 0 and smallerthan 2, with an alkoxy- or aryloxy-containing silane compound to give afirst intermediate reaction product; contacting the first intermediatereaction product with at least one activating compound selected from thegroup of electron donors, compounds of formula M(OR¹⁰)_(v-w)(OR¹¹)_(w)wherein M is Ti, Zr, Hf, Al or Si, and M(OR¹⁰)_(v-w)(R¹¹)_(w) wherein Mis Si, and each R¹⁰ and R₁₁ independently, represent an alkyl, alkenylor aryl group, v is the valency of M, v is 3 or 4, and w is less than v;to give a second intermediate reaction product; and contacting thesecond intermediate reaction product with a halogen-containingTi-compound, a monoester as activating agent, a 1,3-diether as aninternal electron donor, and optionally a diester as an additionalinternal electron donor.
 11. A catalyst system for polymerization ofolefins comprising the catalyst component according to claim 10, aco-catalyst and optionally an external electron donor.
 12. The catalystsystem according to claim 11, wherein no external donor is present. 13.A process for making a polyolefin comprising contacting an olefin withthe catalyst system according to claim
 11. 14. (canceled)
 15. Apolyolefin obtained or by the process for making a polyolefin accordingto claim
 13. 16. The polyolefin of claim 15, wherein said polyolefin ispolypropylene.
 17. The polyolefin of claim 15, wherein said polyolefinis a homopolymer of polypropylene.
 18. The process of claim 13, whereinthe olefin is propylene.
 19. The catalyst component of claim 10, whereinthe at least one activation compound is the compound of formulaM(OR¹⁰)_(v-w)(R¹¹)_(w), wherein M is Si.
 20. The catalyst component ofclaim 10, wherein said monoester is present in an amount less than 4.0wt. %.
 21. The catalyst component of claim 10, wherein said monoester ispresent in an amount of up to 3.5 wt. %.